CN104383704B - A kind of step heating system to the preheating of gas fractionator inlet feed - Google Patents
A kind of step heating system to the preheating of gas fractionator inlet feed Download PDFInfo
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- CN104383704B CN104383704B CN201410483273.6A CN201410483273A CN104383704B CN 104383704 B CN104383704 B CN 104383704B CN 201410483273 A CN201410483273 A CN 201410483273A CN 104383704 B CN104383704 B CN 104383704B
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- heat
- heat exchanger
- inlet feed
- hot water
- fractionating column
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- 238000010438 heat treatment Methods 0.000 title claims abstract description 40
- 239000000463 material Substances 0.000 claims abstract description 98
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 71
- 238000000034 method Methods 0.000 claims abstract description 49
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims abstract description 46
- 239000002918 waste heat Substances 0.000 claims abstract description 32
- 238000010521 absorption reaction Methods 0.000 claims abstract description 23
- 239000007789 gas Substances 0.000 claims abstract description 19
- 238000001816 cooling Methods 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 10
- 238000005194 fractionation Methods 0.000 claims abstract description 8
- 238000004508 fractional distillation Methods 0.000 claims abstract description 5
- 239000000498 cooling water Substances 0.000 claims description 15
- 230000010354 integration Effects 0.000 claims description 14
- 238000007670 refining Methods 0.000 claims description 12
- 238000005516 engineering process Methods 0.000 claims description 6
- 239000006200 vaporizer Substances 0.000 claims description 5
- 239000006096 absorbing agent Substances 0.000 claims description 4
- 230000003134 recirculating effect Effects 0.000 claims description 3
- 239000003208 petroleum Substances 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000008676 import Effects 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 2
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003348 petrochemical agent Substances 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to a kind of step heating system to the preheating of gas fractionator inlet feed, inlet feed system component is heated, wherein: gas fractionation heating system component includes: fractionating column, air cooler, water cooling heat exchanger and reboiler including petroleum fractionating heating system component and recovery waste heat; Recovery waste heat heating inlet feed system component includes: hot water/material heat exchanger and steam type lithium bromide absorption type heat pump; Outer to material pre-heating temperature elevation to 80 ± 10 DEG C at fractionating column by hot water/material heat exchanger, the material after preheating enters fractionating column, is heated by bottom reboiler and maintain the operating temperature needed for material fractional distillation in tower, it is achieved the step heating of material. Its advantage is: utilize the waste heat reclaimed that inlet feed is preheated, it is achieved that the cascaded utilization of energy of fractionating column heating technique, reduces process steam consumption more than 20%, improves energy utilization rate, saved cost.
Description
Technical field
The invention belongs to oil refining production field, relate to a kind of step heating system to the preheating of gas fractionator inlet feed, be related specifically to gas recovery fractionator overhead product material waste heat and other process heats of oil refining combine the system that fractionating column inlet feed step is heated by waste heat.
Background technology
Along with developing rapidly of national economy, society is growing to the demand of petrochemicals, and the sector energy-output ratio accounts for more than the 10% of whole nation energy resource consumption total amount. And in the production of oil refining factory, gas fractionation process link is to use hot rich and influential family, conventional gas fractionation process system flow is as it is shown in figure 1, mainly comprise following major part: fractionating column 1, reboiler 2, air cooler 3, water cooling heat exchanger 4 and for connecting the pipeline of the said equipment, valve etc. Room temperature material is directly entered fractionating column by material inlet P1, bottom reboiler heat and maintain to operating temperature, and the product thermal material of tower top outlet sequentially passes through after air cooler and water cooling heat exchanger cooling to material outlet P2.
Its shortcoming 1 is: the waste heat of the product thermal material (oil gas) of fractionator overhead outlet is lost in environment by air cooler, water cooling heat exchanger and circulation thereof, causes substantial amounts of energy dissipation.
Its shortcoming 2 is: room temperature (about the 20 DEG C) inlet feed of fractionating column heats through bottom reboiler and maintains to operating temperature, the materials at bottom of tower operating temperature of the techniques such as wherein hydramine regeneration, depropanization, catalytic distillation is about 110 DEG C, reboiler generally using pressure be about 0.3MPa process steam as heating heating agent, there is bigger heat transfer temperature difference in this heating mode, the entropy of heating link increases relatively big, and utilizing of the energy is unreasonable.
Summary of the invention
It is an object of the invention to the deficiency for existing fractionating column heating material technological process, it is proposed to a kind of step heating system to the preheating of gas fractionator inlet feed.A kind of step heating system utilizing steam type lithium bromide absorption type heat pump recovery fractionator overhead waste heat that inlet feed is preheated especially set out, hot water can be prepared by efficient recovery fractionator overhead exported product thermal material waste heat, by hot water/material heat exchanger, fractionating column charging be preheated; When there being other stable process procedure heat integration waste heat heat medium water, steam type lithium bromide absorption type heat pump can be replaced as the heat source of hot water/material heat exchanger, fractionating column inlet feed to be preheated. This invention address that the scheme that its technical problem adopts is as follows:
A kind of step heating system utilizing waste heat that gas fractionator inlet feed is preheated, inlet feed system component is heated including gas fractionation heating system component and recovery waste heat, wherein: described gas fractionation heating system component includes: fractionating column, air cooler, water cooling heat exchanger and reboiler, fractionator overhead material outlet connects air cooler material side entrance, air cooler material side outlet water receiving cold heat exchanger material side entrance; Water cooling heat exchanger water side joint recirculating cooling water system; The low temperature side joint fractionating column of reboiler, reboiler high temperature side joint high-temperature technology steam; Described recovery waste heat heating inlet feed system component includes: hot water/material heat exchanger and steam type lithium bromide absorption type heat pump, wherein: hot water/material heat exchanger material side joint fractionating column material inlet, hot water/material heat exchanger hot water side joint steam type lithium bromide absorption type heat pump condenser and absorber, steam type lithium bromide absorption type heat pump generator connects high-temperature technology steam, and steam type lithium bromide absorption type heat pump vaporizer connects recirculated cooling water; Outer to material pre-heating temperature elevation to 80 ± 10 DEG C at fractionating column by hot water/material heat exchanger, the material after preheating enters fractionating column, is heated by bottom reboiler and maintain the operating temperature needed for material fractional distillation in tower, it is achieved the step heating of material.
The heat source of described hot water/material heat exchanger is to reclaim hot water prepared by fractionator overhead exported product thermal material waste heat, or other process procedure heat integration waste heat heat medium water of oil refining.
Operating temperature needed for described material fractional distillation is 110 ± 10 DEG C.
Described steam type lithium bromide absorption type heat pump can be substituted by other process procedure heat integration waste heat heat medium water pipeline of oil refining, wherein: hot water/material heat exchanger low temperature side joint fractionating column material inlet, other process procedure heat integration waste heat heat medium water pipeline of hot water/material heat exchanger high temperature side joint oil refining.
The invention has the beneficial effects as follows: reclaim the fractionator overhead product material waste heat being originally lost in environment, or utilize other process procedure heat integration waste heat of oil refining, for inlet feed is preheated, achieve the cascaded utilization of energy of fractionating column heating technique, reduce process steam consumption more than 20%, improve the efficiency of energy utilization of fractionating column technological process, and then save production cost.
Accompanying drawing explanation
Fig. 1 is conventional fractionation tower process system flow sketch.
Fig. 2 is the fractionating column process system general flow chart utilizing lithium bromide absorption type heat pump and process steam that inlet feed step is heated.
Fig. 3 is the fractionating column process system general flow chart utilizing other process procedure heat integration waste heat heat medium water of oil refining and process steam that inlet feed step is heated.
In figure: 1. fractionating column, 2. reboiler, 3. air cooler, 4. water cooling heat exchanger, 5. hot water/material heat exchanger, 6. steam type lithium bromide absorption type heat pump, 7. valve, P1. material inlet pipeline, P2. overhead product material outlet pipeline, P3. bottom product material outlet pipeline, P4. process steam pipeline, P5, P6. drain water piping, P7. recirculated cooling water high-temperature pipe, P8. recirculated cooling water cryogenic piping, P9. heat integration waste heat heat medium water high-temperature pipe, P10. heat integration waste heat heat medium water cryogenic piping, A. absorber, C. condenser, E. vaporizer, G. generator.
Detailed description of the invention
Below in conjunction with drawings and Examples, the present invention is further described.
Embodiment 1:
In the flow process 2 shown in Fig. 2, material inlet pipeline P1 is connected with the material side entrance 51 of hot water/material heat exchanger 5 and the import of valve 7 respectively, the material inlet 11 of fractionating column 1 exports 52 with the material side of the outlet of valve 7 and hot water/material heat exchanger 5 respectively and is connected, the tower top high-temperature product material outlet 12 of fractionating column 1 is connected with the entrance of air cooler, finished product materials at the bottom of fractionating column 1 tower meets bottom product outlet conduit P3, fractionating column 1 materials at bottom of tower outlet 13 is connected with the low temperature side import 21 of reboiler 2, fractionating column 1 materials at bottom of tower import 14 exports 22 with the low temperature side of reboiler 2 and is connected, the outlet of air cooler 3 is connected with the material inlet 41 of water cooling heat exchanger 4, the material outlet 42 of water cooling heat exchanger 4 is connected with tower top product outlet pipe P2, and the circulating cooling water inlet 43 of water cooling heat exchanger 4 is connected with recirculated cooling water cryogenic piping P8, and circulating cooling water out 44 is connected with recirculated cooling water high-temperature pipe P7, the vaporizer E interface 65,66 of steam type lithium bromide absorption type heat pump 6 is connected with recirculated cooling water high-temperature pipe P7, recirculated cooling water cryogenic piping P8 respectively, absorber A is connected with the high temperature side interface 54,53 of hot water/material heat exchanger respectively with condenser C interface 63,64, and generator G interface 61,62 is connected with process steam pipeline P4, drain water piping P6 respectively, the high temperature side interface 23,24 of reboiler is connected with process steam pipeline P4, drain water piping P5 respectively.
During system work, material is entered hot water/material heat exchanger by material inlet pipeline P1 and is heated, temperature enters fractionating column 1 through material inlet 11 after rising to 80 ± 10 DEG C, is heated by bottom reboiler and maintain to about 110 DEG C in tower, it is achieved the step heating of material. Overhead product arrives product material outlet pipeline P2 through air cooler 3 and water cooling heat exchanger 4 successively; Materials at bottom of tower is exported 13 entrance reboilers 2 by materials at bottom of tower, enters fractionating column 1 through materials at bottom of tower import 14 after heating.
A large amount of waste heats of overhead product material are taken away by recirculating cooling water system by water cooling heat exchanger 4, recirculated cooling water after intensification leads to the vaporizer E of steam type lithium bromide absorption type heat pump 6, low-temperature heat source as steam type lithium bromide absorption type heat pump 6, utilize a small amount of high-temperature technology steam as driving heat source, the middle warm water of preparation, in this, warm water is as the thermal source of hot water/material heat exchanger 5, is achieved in reclaiming the tower top material waste heat lain in recirculated cooling water.
Embodiment 2:
If other technique of oil refining factory (such as Atmospheric vacuum, catalytic cracking) produces the grade more than needed heat integration waste heat heat medium water lower than process steam, steam type lithium bromide absorption type heat pump can be replaced with heat integration heat medium water circulation line P9, P10, thermal source as hot water/material heat exchanger, other connected modes and operation principle are with embodiment 1, and its flow process is as shown in Figure 3.
Hot water/the material heat exchanger 5, steam type lithium bromide absorption type heat pump 6 and the valve 7 that increase newly in the present invention are matured product. The detailed description of the invention of each equipment is respectively described below:
1. fractionating column, determines according to material throughput, for common equipment;
2. reboiler, determines according to material throughput, feeding temperature and Ta Nei temperature of charge, for common equipment;
3. air cooler, determines according to the finished product materials chilling temperature of the volume of production of tower top material, requirement, for common equipment;
4. water cooling heat exchanger, determines according to the finished product materials chilling temperature of the volume of production of tower top material, requirement, for common equipment;
5. hot water/material heat exchanger, determines according to inlet feed flow and heating-up temperature, for non-standard de-sign equipment;
6. steam lithium bromide absorption type heat pump, determines according to calorific requirement and the temperature of process steam pressure, tower top waste heat amount and temperature and hot water/material heat exchanger, this is non-standard de-sign equipment;
7. valve, determines size according to caliber.
The heating system of the present invention is on the basis of the fractionating column original flow process of heating material technique, it is additionally arranged hot water/material heat exchanger in fractionating column material inlet place, utilizing steam type lithium bromide absorption type heat pump gas recovery fractionator overhead waste heat, the step heating procedure 2 that inlet feed is preheated is as shown in Figure 2; Utilize other petrochemical processing heat integration waste heat heat medium water realize inlet feed preheating step heating procedure 3 as shown in Figure 3. The entropy of the fractionating column heating link that the method can reduce the techniques such as hydramine regeneration, depropanization, catalytic distillation increases, it is achieved, the Appropriate application of the energy, save and produce the process steam consumed.
Claims (4)
1. the step heating system to the preheating of gas fractionator inlet feed, inlet feed system component is heated including gas fractionation heating system component and recovery waste heat, wherein: described gas fractionation heating system component includes: fractionating column, air cooler, water cooling heat exchanger and reboiler, fractionator overhead material outlet connects air cooler material side entrance, air cooler material side outlet water receiving cold heat exchanger material side entrance; Water cooling heat exchanger water side joint recirculating cooling water system; The low temperature side joint fractionating column of reboiler, reboiler high temperature side joint high-temperature technology steam, it is characterized in that: described recovery waste heat heating inlet feed system component includes: hot water/material heat exchanger and steam type lithium bromide absorption type heat pump, wherein: hot water/material heat exchanger material side joint fractionating column inlet feed, hot water/material heat exchanger hot water side joint steam type lithium bromide absorption type heat pump condenser and absorber, steam type lithium bromide absorption type heat pump generator connects high-temperature technology steam, and steam type lithium bromide absorption type heat pump vaporizer connects recirculated cooling water; Outer to material pre-heating temperature elevation to 80 ± 10 DEG C at fractionating column by hot water/material heat exchanger, the material after preheating enters fractionating column, is heated by bottom reboiler and maintain the temperature needed for material fractional distillation in tower, it is achieved the step heating of material.
2. the step heating system to the preheating of gas fractionator inlet feed according to claim 1, it is characterized in that: the heat source of described hot water/material heat exchanger is to utilize steam type lithium bromide absorption type heat pump to reclaim hot water prepared by fractionator overhead exported product thermal material waste heat or other process procedure heat integration waste heat heat medium water of oil refining.
3. the step heating system to the preheating of gas fractionator inlet feed according to claim 1, is characterized in that: the operating temperature needed for described material fractional distillation is 110 ± 10 DEG C.
4. the step heating system to the preheating of gas fractionator inlet feed according to claim 1, it is characterized in that: described steam type lithium bromide absorption type heat pump can be substituted by other process procedure heat integration waste heat heat medium water pipeline of oil refining, wherein: hot water/material heat exchanger low temperature side joint fractionating column inlet feed, other process procedure heat integration waste heat heat medium water pipeline of hot water/material heat exchanger high temperature side joint oil refining.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410483273.6A CN104383704B (en) | 2014-09-19 | 2014-09-19 | A kind of step heating system to the preheating of gas fractionator inlet feed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410483273.6A CN104383704B (en) | 2014-09-19 | 2014-09-19 | A kind of step heating system to the preheating of gas fractionator inlet feed |
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| CN104383704A CN104383704A (en) | 2015-03-04 |
| CN104383704B true CN104383704B (en) | 2016-06-15 |
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| CN201410483273.6A Expired - Fee Related CN104383704B (en) | 2014-09-19 | 2014-09-19 | A kind of step heating system to the preheating of gas fractionator inlet feed |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108079611B (en) * | 2018-02-08 | 2019-07-05 | 燕山大学 | A kind of intermediate reboiler step heating system based on absorption heat pump |
| CN111925816A (en) * | 2020-07-22 | 2020-11-13 | 山东益大新材料股份有限公司 | Production method of low CTE coal-series needle coke |
| CN112169364B (en) * | 2020-09-29 | 2021-12-24 | 江苏博颂化工科技有限公司 | Fractionating tower heat pump system adopting external circulating working medium |
| CN113289365B (en) * | 2021-07-01 | 2022-06-17 | 燕山大学 | Absorption heat pump rectification system based on intermediate reboiling and intermediate condensation |
| CN113666377B (en) * | 2021-09-30 | 2023-03-10 | 四川永祥多晶硅有限公司 | Comprehensive energy utilization method for polycrystalline silicon tail gas |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103446775A (en) * | 2013-07-24 | 2013-12-18 | 杭州电子科技大学 | Control system of novel distilling and condensation energy-conservation process |
| CN103446774A (en) * | 2013-07-24 | 2013-12-18 | 李少兵 | Distillation and condensation energy-saving technology based on heat pump technology |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103446775A (en) * | 2013-07-24 | 2013-12-18 | 杭州电子科技大学 | Control system of novel distilling and condensation energy-conservation process |
| CN103446774A (en) * | 2013-07-24 | 2013-12-18 | 李少兵 | Distillation and condensation energy-saving technology based on heat pump technology |
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